CN108585089A - A kind of sodium chloride ammonium chloride divides salt crystallization processes and device - Google Patents
A kind of sodium chloride ammonium chloride divides salt crystallization processes and device Download PDFInfo
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- CN108585089A CN108585089A CN201810507176.4A CN201810507176A CN108585089A CN 108585089 A CN108585089 A CN 108585089A CN 201810507176 A CN201810507176 A CN 201810507176A CN 108585089 A CN108585089 A CN 108585089A
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01C—AMMONIA; CYANOGEN; COMPOUNDS THEREOF
- C01C1/00—Ammonia; Compounds thereof
- C01C1/16—Halides of ammonium
- C01C1/164—Ammonium chloride
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
- C01D3/00—Halides of sodium, potassium or alkali metals in general
- C01D3/14—Purification
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/10—Inorganic compounds
- C02F2101/12—Halogens or halogen-containing compounds
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/10—Inorganic compounds
- C02F2101/16—Nitrogen compounds, e.g. ammonia
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2301/00—General aspects of water treatment
- C02F2301/08—Multistage treatments, e.g. repetition of the same process step under different conditions
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- Environmental & Geological Engineering (AREA)
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- Heat Treatment Of Water, Waste Water Or Sewage (AREA)
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
The invention discloses a kind of sodium chloride ammonium chlorides to divide salt crystallization processes, sodium chloride is crystallized be precipitated at high operating temperatures by the technique, oversaturated ammonium chloride is precipitated under low-temperature condition, to realize the separation and recycling of sodium chloride in waste water, ammonium chloride, the sodium chloride and ammonium chloride product of technical grade are obtained, the generation of solid waste or dangerous waste is reduced, no emission for causing river pollution has achieved the effect that the resource reclaim of no pollution liquid discharge.Sodium chloride ammonium chloride provided by the invention divides salt crystallization apparatus, and structure setting is reasonable, saves energy consumption, is easily achieved, high degree of automation, operating cost is low, can be widely applied to during actual industrial production.
Description
Technical field
The present invention relates to environment-protection wastewater recovery technology fields, and in particular to a kind of sodium chloride ammonium chloride divide salt crystallization processes and
Device.
Background technology
Waste water is the general name of the water being discharged in people's active procedure and runoff rainwater, generally comprises sanitary sewage, industry
Waste water and diameter flow into the other useless water of rainwater grade of drainpipe, belong to one of big public hazards of orchid of nature, wherein industrial wastewater is
The waste water and waste liquid generated in the industrial production contains industrial production materials, intermediate product, byproduct and the life outflowed with water
The pollutant generated in the process is produced, with the rapid development of industry, the type and quantity of waste water rapidly increase, the pollution to water body
Also increasingly extensively and serious, the health and safety of the mankind is threaten, while also containing a large amount of recoverable resources in sewage, such as
It is not recycled, will bring about great losses, therefore sewage is developed and comprehensively utilized, turning harm into good is particularly important.
Metallurgical Waste Water, chemical waste water main component are substantially inorganic salts and all kinds of mixed salts, in production as industry is raw
Produce device continuous construction, sewage, exhaust gas, waste discharge capacity be also continuously increased, however the whole world environmental issue increasingly
Seriously, the continuous increase of environmentally friendly dynamics, so resource recovery process is also constantly being promoted.Currently, although each enterprise is actively equipped with
Evaporated crystallization device handles high-salt wastewater, but still remains many problems.The technique that enterprise uses at present is to have recycled absolutely mostly
Most water has simultaneously obtained crystal salt, but since obtained crystal salt is carnallite, it not only cannot be by recycling instead
Understand according to the qualitative disposition of dangerous waste, meanwhile, liquid waste processing is not thorough, and still has a large amount of separating liquids to need to discharge, and discharging of waste liquid is still
River pollution, processing procedure high energy consumption, these problems can be caused to annoying enterprise, and seriously affected the project process of enterprise,
Zero liquid of high-salt wastewater discharges and recycling treatment is the inexorable trend of high-salt wastewater improvement.
Mixed salt is formed after existing sodium chloride ammonium chloride evaporation, dangerous waste processing can only be done, Nacl cannot be done.Dangerous waste processing
It needs to spend a large amount of disposal costs, and Nacl can generate economic benefit.
Invention content
In order to solve the above technical problems, we have proposed a kind of sodium chloride ammonium chlorides to divide salt crystallization processes and device, solve
Carnallite forms solid waste, causes environmental pollution in the prior art, reaches reduction pollution, improves water reuse rate, reduces at solid waste
Manage the purpose of cost.
In order to achieve the above objectives, technical scheme is as follows：
A kind of sodium chloride ammonium chloride divides salt crystallization processes, includes the following steps：
S1. it preheats, 90 DEG C -100 DEG C is tentatively preheated to the waste water of sodium chloride-containing ammonium chloride；
S2. it is concentrated by evaporation and obtains oversaturated sodium chloride waste water, the waste water after being preheated to S1 further heats, then gas-liquid
Separation, being concentrated by evaporation makes the sodium chloride of liquid phase reach concentrate supersaturated and that ammonium chloride is undersaturated condition；
S3. Isolating chlorinated sodium is centrifugally separating to obtain chlorination after further being thickened to the supersaturated sodium chloride waste water that S2 is obtained
Sodium crystal and one-level mother liquor；
S4. it is concentrated by evaporation and obtains oversaturated ammonium chloride waste-water, the one-level mother liquor that S3 is obtained is heated, then gas-liquid
Separation, evaporation and concentration make the ammonium chloride of liquid phase reach supersaturation；
S5. separating ammonium chloride carries out frozen cooling to the one-level mother liquor that S4 is obtained, is further centrifugally separating to obtain after thickening
Ammonia chloride crystal and secondary mother liquor.
S6. Recycling Mother Solution, the secondary mother liquor reuse after S5 is detached are evaporated concentration again to step S2.
Further, sodium chloride concentration ＞ 28.5% in step S2, ammonium chloride concentration ＜ 35%.
Further, 45% ＜ ammonium chloride concentrations ＜ 35% in step S4.
Further, the temperature range of frozen cooling is 20-40 DEG C in step S5
Further, a concentration of sodium chloride≤15% of the secondary mother liquor in step S5, ammonium chloride≤25%.
A kind of sodium chloride ammonium chloride divides the device of salt crystallization processes, including pre-heating system connected in sequence, sodium chloride crystal
System is precipitated in precipitation system and ammonia chloride crystal, and system and ammonia chloride crystal precipitation system is precipitated with sodium chloride crystal respectively
Carry out the vapour compression machine of heat exchange.
The pre-heating system includes raw material surge tank, feed pump, hot water preheater, vapor preheater, condensate pump and cold
Condensate tank, wherein the raw material surge tank, the feed pump, the hot water preheater and the vapor preheater are sequentially connected with,
System and ammonia chloride crystal precipitation is precipitated from vapor preheater, the sodium chloride crystal for receiving in the condensate water pot
The condensed water of system, the condensate pump are used to the condensed water in the condensate water pot being delivered to hot water preheater as heat
Source.
It includes primary heater, primary cycle pump, primary separator, level-one discharging that system, which is precipitated, in the sodium chloride crystal
Pump, level-one thickener, first-stage centrifugal machine, one-level mother liquor tank and level-one discharging pump, the side wall of the primary separator is from top to bottom
It is equipped with first charging aperture, second charging aperture, third feed inlet and the 4th feed inlet successively, the first charging aperture is come for receiving
The waste liquid of system is precipitated from the ammonia chloride crystal；It is equipped between the third feed inlet and the feed inlet of the primary heater
Primary cycle pipe；
The waste liquid preheated through the vapor preheater is delivered to the primary cycle pipe, and wherein gas phase enters a fraction
From in device, liquid phase enters in the primary heater；Material in the primary heater is pumped by the primary cycle to be conveyed
To the second charging aperture；The level-one discharging pump is used to the material of the primary separator being delivered to the level-one thickener
In；The feed end of the discharge end of the primary separator and the level-one thickener is equipped with level-one return duct, is convenient for the level-one
Partial Liquid Phase is converted into gas phase when liquid phase in separator is delivered to the level-one thickener through the level-one discharging pump, and gas phase is just
Enter in the primary separator from the level-one return duct；
The first-stage centrifugal machine is used to the material in the level-one thickener being separated by solid-liquid separation, and it is female that liquid enters the level-one
Flow container is pumped into the ammonia chloride crystal through the level-one discharging pump and system is precipitated.
It includes secondary heater, secondary cycle pump, second-stage separator, two level discharging that system, which is precipitated, in the ammonia chloride crystal
Pump, two level thickener, two-stage centrifugal machine, secondary mother liquor tank and two level discharging pump, the side wall of the second-stage separator is from top to bottom
It is equipped with feed inlet one, feed inlet two and feed inlet three successively, between the feed inlet two and the feed inlet of the secondary heater
Equipped with secondary cycle pipe；
Waste liquid is pumped into the secondary cycle pipe by the level-one discharging pump, and wherein gas phase enters in the second-stage separator,
Liquid phase enters in the secondary heater；Material in the secondary heater by secondary cycle pump be delivered to it is described into
Material mouth one；Material in the second-stage separator is delivered to through the two level discharging pump in the two level thickener；
The feed end of the discharge end of the second-stage separator and the two level thickener is equipped with two level return duct, convenient for described
Partial Liquid Phase is converted into gas phase, gas when liquid phase in second-stage separator is delivered to the two level thickener through the two level discharging pump
Mutually just enter in second-stage separator from the two level return duct；
The two-stage centrifugal machine is used to the material in the two level thickener being separated by solid-liquid separation, and it is female that liquid enters the two level
Flow container is pumped into the primary separator through the first charging aperture through the two level discharging pump and continues circulating and evaporating concentration.
Further, the two level thickener is equipped with the low-temperature receiver that can cool down.
Technical scheme of the present invention has the following advantages compared with prior art：
Chlorine drops in the technique of the present invention that sodium chloride, ammonium chloride are recycled from waste water, the technique at high operating temperatures
Change sodium crystallization to be precipitated, oversaturated ammonium chloride is precipitated under low-temperature condition, to realize sodium chloride in waste water, ammonium chloride
Separation and recycling, have obtained the sodium chloride and ammonium chloride product of technical grade, reduce the generation of solid waste or dangerous waste, no initiation water system
The emission of pollution has reached the technique effect of the resource reclaim of no pollution liquid discharge.
Device of the present invention for the technique of recycling receipts sodium chloride, ammonium chloride from waste water, using energy-efficient machine
The energy consumption of tool steam recompression technology, 1 ton of water of evaporation is about 1/6 to the 1/5 of conventional evaporator, and the thermal efficiency is high, low in energy consumption, adopts
With mechanical vapor recompression technology, is heated using less amount of fresh steam, reduce the dependence to boiler plant, reduce pollution
Object, it is environmentally safe, it is more energy-saving and environmentally friendly.
Present invention process flow is simple, it is easy to accomplish, high degree of automation, operating cost is low, meets sustainable development and wants
It asks, can be widely applied to during actual industrial production.
Description of the drawings
In order to more clearly explain the embodiment of the invention or the technical proposal in the existing technology, to embodiment or will show below
There is attached drawing needed in technology description to be briefly described, it should be apparent that, the accompanying drawings in the following description is only this
Some embodiments of invention for those of ordinary skill in the art without creative efforts, can be with
Obtain other attached drawings according to these attached drawings.
Fig. 1 divides the schematic diagram of the device of salt crystallization processes for a kind of sodium chloride ammonium chloride disclosed in the embodiment of the present invention.
Number and the corresponding component title represented by letter in figure：
1. 2. 4. condensate pump of feed pump 3-1. hot water preheater 3-2. vapor preheaters of raw material surge tank, 5. level-one
6. primary cycle of heater pumps 7. primary separator 7-1. primary cycle pipe 7-2 level-ones return duct, 8. level-one discharging pump 9.
11. one-level mother liquor tank of level-one thickener 9-1 level-ones 10. first-stage centrifugal machine of bursting tube, 12. one-level mother liquor pumps 13. two levels and adds
14 secondary cycle of hot device pumps 15. second-stage separator 15-1 secondary cycle pipe 15-2 two levels return duct, 16. two level discharging pump
17. 19. secondary mother liquor tank of two level thickener 17-1 secondary safeties 18. two-stage centrifugal machine of pipe, 20. secondary mother liquor pump 21. steams
22. condensate water pot a. cooling water inlet b. cooling water outlets of vapour compressor
Specific implementation mode
Following will be combined with the drawings in the embodiments of the present invention, and technical solution in the embodiment of the present invention carries out clear, complete
Site preparation describes, it is clear that described embodiments are only a part of the embodiments of the present invention, instead of all the embodiments.It is based on
Embodiment in the present invention, those of ordinary skill in the art are obtained every other without creative efforts
Embodiment shall fall within the protection scope of the present invention.
With reference to embodiment and specific implementation mode, the present invention is described in further detail.
Embodiment 1
As shown in Figure 1, a kind of sodium chloride ammonium chloride divides salt crystallization processes, sodium chloride mass fraction is 6.08% in waste water,
Ammonium chloride mass fraction is 5.35%, and the total flow of waste water is 10.8t/h, is included the following steps：
S1. it preheats, waste water squeezes into preheater by feed pump 2 by raw material surge tank 1 and tentatively heated up, and heating is divided into two
Step：Waste water first passes through hot water preheater (hot water plate type preheater) 3-1 heating, the high-temperature condensation water that heat source is 105 DEG C, waste liquid
It can be heated to 82 DEG C；It is heated using vapor preheater (i.e. steam-plate type preheater) 3-2, the steam that this heat source is 110 DEG C gives up
Water can be heated to 93-95 DEG C；
S2. it is concentrated by evaporation and obtains oversaturated sodium chloride waste water, the waste water after being preheated in step S1 is via primary separator 7
Primary cycle pipe 7-1 enter primary heater 5 and carry out heat exchange heating, the waste liquid after heating is delivered to one through primary cycle pump 6
In grade separator 7, waste liquid interior progress gas-liquid separation (about 85 DEG C of gas phase temperature, about 94 DEG C of liquidus temperature) in primary separator 7,
Evaporation and concentration makes the sodium chloride of liquid phase reach supersaturation, and (ammonium chloride is unsaturated solution, control sodium chloride concentration ＞ at this time
28.5%, ammonium chloride concentration ＜ 35%) when, by level-one discharging pump 8, squeeze into level-one thickener 9, at the same time, gas phase into
Enter the recompression of vapour compression machine 21,85 DEG C of 21 inlet temperature of vapour compression machine, 105 DEG C of outlet temperature；
S3. Isolating chlorinated sodium, level-one thickener 9 is to oversaturated sodium chloride waste water (the sodium chloride concentration ＞ that is obtained in S2
28.5%, ammonium chloride concentration ＜ 35%) further thickening after squeeze into first-stage centrifugal machine 10, sodium chloride crystal passes through first-stage centrifugal machine
10 are centrifuged out, and the sodium chloride liquid of low concentration, which enters one-level mother liquor tank 11, becomes one-level mother liquor；
S4. it is concentrated by evaporation and obtains oversaturated ammonium chloride waste-water, it will be in one-level mother liquor tank 11 by one-level mother liquor pump 12
One-level mother liquor squeezes into the secondary cycle pipe 15-1 of second-stage separator 15, enters two by the secondary cycle pipe 15-1 of second-stage separator 15
Grade heater 13, carries out heat exchange heating (temperature is heated to 100 DEG C or so), and the waste liquid after heating is delivered to through secondary cycle pump 14
In second-stage separator 15, waste liquid carries out gas-liquid separation, about 85 DEG C of gas phase temperature, liquidus temperature about 100 in second-stage separator 15
DEG C, when evaporation and concentration makes the ammonium chloride of liquid phase reach supersaturation (ammonium chloride concentration ＞ 35% is controlled 45% or so), pass through two
Grade discharging pump 16, squeezes into two level thickener 17, and gas phase enters the recompression of vapour compression machine 21；Vapour compression machine inlet temperature 85
DEG C, 105 DEG C of outlet temperature；
S5. separating ammonium chloride, two level thickener 17 are cooled to by circulating water cooling to continuing through chilled water after 40 DEG C
25 DEG C (chilled waters from cooling water inlet a into go out from cooling water outlet b), liquid further squeeze into two-stage centrifugal machine 18 after thickening,
Ammonia chloride crystal is centrifuged out by two-stage centrifugal machine 18, and mother liquor, which enters secondary mother liquor tank 19, becomes secondary mother liquor.
S6. Recycling Mother Solution, the secondary mother liquor (9.8% sodium chloride, 18.2% ammonium chloride) after S5 is detached pass through two
In grade mother liquor pump 20 reuses to the primary separator 7 of step S2, it is evaporated concentration again.
Further, the feed end of the discharge end of primary separator 7 and level-one thickener 9 is equipped with level-one return duct 7-2,
Partial Liquid Phase is converted into gas phase, gas when being delivered to level-one thickener 9 through level-one discharging pump 8 convenient for the liquid phase in primary separator 7
Mutually just enter in primary separator 7 from level-one return duct 7-2.The setting of level-one return duct 7-2 is not only convenient for the reflux of gas phase,
And be conducive to the safety of lifting device, maintain the pressure balance of level-one thickener and whole system.
Further, the level-one bursting tube for gas-liquid equilibrium is connected between level-one thickener 9 and one-level mother liquor tank 11
9-1 can be obviously improved the safety of system.
Likewise, the discharge end of second-stage separator 15 and the feed end of two level thickener 17 are equipped with two level return duct 15-1,
Partial Liquid Phase is converted into gas phase, gas when being delivered to two level thickener 17 through two level discharging pump convenient for the liquid phase in second-stage separator 15
Mutually just enter in second-stage separator 15 from two level return duct 15-1.The setting of two level return duct is not only convenient for the reflux of gas phase,
And be conducive to the safety of lifting device, maintain the pressure balance of two level thickener and whole system.
Primary heater 5 and secondary heater 13 exchange heat after high-temperature condensation water (about 95 DEG C) and vapor preheater 3-2
Hot water (about 105 DEG C of steam condensate (SC), specifically by vapor (steam) temperature depending on) is condensed, into condensate water pot 22, in condensate water pot 22
High-temperature condensation water by condensate pump 4 squeeze into hot water preheater 3-1 be used as preheater heat source heat exchange after condensed water (about 40
DEG C) go out battery limit (BL).
In this example, hot water plate type preheater 3-1 is using (heat exchange area：50m2, single process, plate thickness 0.6mm；Plate
Material TA2, gasket material EPDM), heat source is the time condensation liquid of forced-circulation evaporator (which refers to), steam-plate type preheating
Device 3-2 is using (heat exchange area：15m2, single process, plate thickness 0.6mm；Plate material TA2, gasket material EPDM), heat source is
105~115 DEG C of steam, flow are about 350kg/h.
Table 1
It can be seen that from upper table, after this technique high salinity wastewater treatment, sodium chloride, the sodium chloride rate of recovery are high, to
So that low energy consumption.
The present embodiment additionally provides the device that a kind of sodium chloride ammonium chloride divides salt crystallization processes comprising connected in sequence pre-
Hot systems, sodium chloride crystal are precipitated system and ammonia chloride crystal and are precipitated system, and be precipitated respectively with sodium chloride crystal system and
The vapour compression machine that system carries out heat exchange is precipitated in ammonia chloride crystal.
The pre-heating system includes raw material surge tank 1, feed pump 2, hot water preheater 3-1, vapor preheater 3-2, condensation
Water pump 4 and condensate water pot 22, wherein raw material surge tank 1, feed pump 2, hot water preheater 3-1 and vapor preheater 3-2 sequentially connect
It connects, system and ammonia chloride crystal precipitation system is precipitated from vapor preheater 3-2 and sodium chloride crystal for receiving in condensate water pot 22
The condensed water of system, condensate pump 4 are used to the condensed water in condensate water pot 22 being delivered to hot water preheater 3-1 as heat source；
The sodium chloride crystal precipitation system includes primary heater 5, primary cycle pumps 6, primary separator 7, level-one goes out
Material pump 8, level-one thickener 9, first-stage centrifugal machine 10, one-level mother liquor tank 11 and level-one discharging pump 12, primary heater 5 and a fraction
It is vertically arranged from device 7, the top of primary heater 5 is feed inlet, and bottom end is discharge port；The top of primary separator 7 is
Gaseous phase outlet, bottom end are discharge port, the side wall of primary separator 7 be equipped with successively from top to bottom first charging aperture, second charging aperture,
Third feed inlet and the 4th feed inlet, first charging aperture are used to receive the waste liquid that system is precipitated from ammonia chloride crystal；Third into
Circulation pipe 7-1 is equipped between material mouth and the feed inlet of primary heater；
Waste liquid through vapor preheater 3-2 preheatings is delivered to circulation pipe 7-1, and wherein gas phase enters in primary separator 7, liquid
Mutually enter in primary heater 5；Material in primary heater 5 is delivered to second charging aperture by primary cycle pump 6；Level-one goes out
Material pump 8 is for the material of primary separator 7 to be delivered in level-one thickener 9；The discharge end and level-one stiff of primary separator 7
The feed end of device 9 is equipped with level-one return duct 7-2, and it is thick through level-one discharging pump 8 to be delivered to level-one convenient for the liquid phase in primary separator 7
Partial Liquid Phase is converted into gas phase when thick device 9, and gas phase just enters from level-one return duct 7-2 in primary separator 7；
For first-stage centrifugal machine 10 for centrifuging out the material in level-one thickener 9, mother liquor enters one-level mother liquor tank
11, it is pumped into ammonia chloride crystal through level-one discharging pump 12 and system is precipitated.
It includes secondary heater 13, secondary cycle pump 14, second-stage separator 15, two level that system, which is precipitated, in the ammonia chloride crystal
Discharging pump 16, two level thickener 17, two-stage centrifugal machine 18, secondary mother liquor tank 19 and two level discharging pump 20,13 He of secondary heater
Second-stage separator 15 is vertically arranged, and the top of secondary heater 13 is feed inlet, and bottom end is discharge port；Second-stage separator 15
Top be gaseous phase outlet, bottom end is discharge port, and the side wall of second-stage separator 15 is equipped with feed inlet one, charging successively from top to bottom
Mouth two and feed inlet three are equipped with circulation pipe 15-1 between feed inlet two and the feed inlet of secondary heater 13；
Waste liquid is pumped into circulation pipe 15-1 by level-one discharging pump 12, and wherein gas phase enters in second-stage separator 15, and liquid phase enters
In secondary heater 13；Material in secondary heater 13 is delivered to feed inlet one by secondary cycle pump 14；Second-stage separator
Material in 15 is delivered to through two level discharging pump 16 in two level thickener 17；The discharge end of second-stage separator and two level thickener
Feed end is equipped with two level return duct 15-2, when being delivered to two level thickener through two level discharging pump convenient for the liquid phase in second-stage separator
Partial Liquid Phase is converted into gas phase, and gas phase just enters from the two level return duct in second-stage separator；
For two-stage centrifugal machine for centrifuging out the material in two level thickener, mother liquor enters secondary mother liquor tank, warp
Two level discharging pump, which is pumped into through first charging aperture in primary separator 7, continues circulating and evaporating concentration.
Wherein, two level thickener 17 be equipped with cooling water inlet a and cooling water outlet b, for be passed through low-temperature cooling water or its
The media such as its refrigerated brine cool down property.
Embodiment 2
As shown in Figure 1, apparatus structure in this example, with embodiment 1, this will not be repeated here.
A kind of sodium chloride ammonium chloride divides salt crystallization processes, and sodium chloride mass fraction is 5.53% in waste water, ammonium chloride quality
Score is 7.02%, and the total flow of waste water is 24.78t/h, is included the following steps：
S1. it preheats, waste water squeezes into preheater by feed pump 2 by raw material surge tank 1 and tentatively heated up, and heating is divided into two
Step：Waste water first passes through hot water preheater (hot water plate type preheater) 3-1 heating, the high-temperature condensation water that heat source is 105 DEG C, waste liquid
It can be heated to 81 DEG C；It is heated using vapor preheater (i.e. steam-plate type preheater) 3-2, the steam that this heat source is 110 DEG C gives up
Water can be heated to 95 DEG C；
S2. it is concentrated by evaporation and obtains oversaturated sodium chloride waste water, the waste water after being preheated in step S1 is via primary separator 7
Circulation pipe 7-1 enter primary heater 5 and carry out heat exchange heating, the waste liquid after heating is delivered to a fraction through primary cycle pump 6
From in device 7, waste liquid interior progress gas-liquid separation (about 85 DEG C of gas phase temperature, about 94 DEG C of liquidus temperature) in primary separator 7 is evaporated
Concentration makes the sodium chloride of liquid phase reach supersaturation, and (ammonium chloride is unsaturated solution, control sodium chloride concentration ＞ 28.5%, chlorine at this time
Change ammonium concentration ＜ 35%) when, it by level-one discharging pump 8, squeezes into level-one thickener 9, at the same time, gas phase enters both vapor compression
Machine 21 recompresses, 85 DEG C of 21 inlet temperature of vapour compression machine, 105 DEG C of outlet temperature；
S3. Isolating chlorinated sodium, level-one thickener 9 is to oversaturated sodium chloride waste water (the sodium chloride concentration ＞ that is obtained in S2
28.5%, ammonium chloride concentration ＜ 35%) further thickening after squeeze into first-stage centrifugal machine 10, sodium chloride crystal passes through first-stage centrifugal machine
10 are centrifuged out, and the sodium chloride liquid of low concentration, which enters one-level mother liquor tank 11, becomes one-level mother liquor；
S4. it is concentrated by evaporation and obtains oversaturated ammonium chloride waste-water, it will be in one-level mother liquor tank 11 by one-level mother liquor pump 12
One-level mother liquor squeezes into the secondary cycle pipe 15-1 of second-stage separator 15, enters two by the secondary cycle pipe 15-1 of second-stage separator 15
Grade heater 13, carries out heat exchange heating (temperature is heated to 100 DEG C or so), and the waste liquid after heating is delivered to through secondary cycle pump 14
In second-stage separator 15, waste liquid carries out gas-liquid separation, about 85 DEG C of gas phase temperature, liquidus temperature about 100 in second-stage separator 15
DEG C, when evaporation and concentration makes the ammonium chloride of liquid phase reach supersaturation (ammonium chloride concentration ＞ 35% is controlled 45% or so), pass through two
Grade discharging pump 16, squeezes into two level thickener 17, and gas phase enters the recompression of vapour compression machine 21；Vapour compression machine inlet temperature 85
DEG C, 105 DEG C of outlet temperature；
S5. separating ammonium chloride, two level thickener 17 are cooled to by circulating water cooling to continuing through chilled water after 40 DEG C
25 DEG C, liquid squeezes into two-stage centrifugal machine 18 after further thickening, and ammonia chloride crystal is centrifuged out by two-stage centrifugal machine 18, mother liquor
Become secondary mother liquor into secondary mother liquor tank 19.
S6. Recycling Mother Solution, the secondary mother liquor (9.8% sodium chloride, 18.2% ammonium chloride) after S5 is detached pass through two
In grade mother liquor pump 20 reuses to the primary separator 7 of step S2, it is evaporated concentration again.
Primary heater 5 and secondary heater 13 exchange heat after high-temperature condensation water (about 95 DEG C) and vapor preheater 3-2
Hot water (about 105 DEG C of steam condensate (SC), specifically by vapor (steam) temperature depending on) is condensed, into condensate water pot 22, in condensate water pot 22
High-temperature condensation water by condensate pump 4 squeeze into hot water preheater 3-1 be used as preheater heat source heat exchange after condensed water (about 40
DEG C) go out battery limit (BL).
In this example, hot water plate type preheater is using (heat exchange area：110m2, single process, plate thickness 0.6mm；Sheet
Matter TA2, gasket material EPDM), heat source be forced-circulation evaporator time condensation liquid, steam-plate type preheater using
(heat exchange area：35m2, single process, plate thickness 0.6mm；Plate material TA2, gasket material EPDM), heat source is 105~115 DEG C
Steam, flow are about 800kg/h.
Table 2
It can be seen that from upper table, after this technique high salinity wastewater treatment, sodium chloride, the sodium chloride rate of recovery are high, to
So that low energy consumption.
What has been described above is only a preferred embodiment of the present invention, it is noted that for those of ordinary skill in the art
For, without departing from the concept of the premise of the invention, various modifications and improvements can be made, these belong to the present invention
Protection domain.
Claims (10)
1. a kind of sodium chloride ammonium chloride divides salt crystallization processes, which is characterized in that include the following steps：
S1. it preheats, 90 DEG C -100 DEG C is tentatively preheated to the waste water of sodium chloride-containing ammonium chloride；
S2. it is concentrated by evaporation and obtains oversaturated sodium chloride waste water, the waste water after being preheated to S1 further heats, then gas-liquid point
From being concentrated by evaporation makes the sodium chloride of liquid phase reach concentrate supersaturated and that ammonium chloride is undersaturated condition；
S3. Isolating chlorinated sodium is centrifugally separating to obtain sodium chloride crystalline substance after further being thickened to the supersaturated sodium chloride waste water that S2 is obtained
Body and one-level mother liquor；
S4. it is concentrated by evaporation and obtains oversaturated ammonium chloride waste-water, the one-level mother liquor that S3 is obtained is heated, then gas-liquid point
From evaporation and concentration makes the ammonium chloride of liquid phase reach supersaturation；
S5. separating ammonium chloride carries out frozen cooling to the one-level mother liquor that S4 is obtained, is further centrifugally separating to obtain chlorination after thickening
Ammonium crystal and secondary mother liquor.
S6. Recycling Mother Solution, the secondary mother liquor reuse after S5 is detached are evaporated concentration again to step S2.
2. a kind of sodium chloride ammonium chloride according to claim 1 divides salt crystallization processes, which is characterized in that chlorination in step S2
Na concn ＞ 28.5%, ammonium chloride concentration ＜ 35%.
3. a kind of sodium chloride ammonium chloride according to claim 1 divides salt crystallization processes, which is characterized in that 45% in step S4
＜ ammonium chloride concentrations ＜ 35%.
4. a kind of sodium chloride ammonium chloride according to claim 1 divides salt crystallization processes, which is characterized in that freezed in step S5
The temperature range of cooling is 20-40 DEG C.
5. a kind of sodium chloride ammonium chloride according to claim 1 divides salt crystallization processes, which is characterized in that two in step S5
A concentration of sodium chloride≤15% of grade mother liquor, ammonium chloride≤25%.
6. a kind of device for being used for a kind of sodium chloride ammonium chloride as claimed in any one of claims 1 to 6 and dividing salt crystallization processes,
It is characterized in that, including system is precipitated for pre-heating system connected in sequence, sodium chloride crystal and system, Yi Jifen is precipitated in ammonia chloride crystal
System is not precipitated with sodium chloride crystal and the vapour compression machine that system carries out heat exchange is precipitated in ammonia chloride crystal.
7. a kind of sodium chloride ammonium chloride according to claim 6 divides the device of salt crystallization processes, which is characterized in that described pre-
Hot systems include raw material surge tank, feed pump, hot water preheater, vapor preheater, condensate pump and condensate water pot, wherein institute
It states raw material surge tank, the feed pump, the hot water preheater and the vapor preheater to be sequentially connected with, the condensate water pot is used
System is precipitated from vapor preheater, the sodium chloride crystal in reception and the condensed water of system is precipitated in the ammonia chloride crystal,
The condensate pump is used to the condensed water in the condensate water pot being delivered to hot water preheater as heat source.
8. a kind of sodium chloride ammonium chloride according to claim 6 divides the device of salt crystallization processes, which is characterized in that the chlorine
It includes primary heater, primary cycle pump, primary separator, level-one discharging pump, level-one thickener, one to change sodium crystal system is precipitated
The side wall of grade centrifuge, one-level mother liquor tank and level-one discharging pump, the primary separator is equipped with the first charging successively from top to bottom
Mouth, second charging aperture, third feed inlet and the 4th feed inlet, the first charging aperture come from the ammonia chloride crystal for receiving
The waste liquid of precipitation system；Primary cycle pipe is equipped between the third feed inlet and the feed inlet of the primary heater；
The waste liquid preheated through the vapor preheater is delivered to the primary cycle pipe, and wherein gas phase enters the primary separator
In, liquid phase enters in the primary heater；Material in the primary heater is delivered to institute by primary cycle pump
State second charging aperture；The level-one discharging pump is for the material of the primary separator to be delivered in the level-one thickener；
The feed end of the discharge end of the primary separator and the level-one thickener is equipped with level-one return duct, is detached convenient for the level-one
Partial Liquid Phase is converted into gas phase when liquid phase in device is delivered to the level-one thickener through the level-one discharging pump, and gas phase is just from institute
Level-one return duct is stated to enter in the primary separator；
The first-stage centrifugal machine is used to the material in the level-one thickener being separated by solid-liquid separation, and liquid enters the one-level mother liquor
Tank is pumped into the ammonia chloride crystal through the level-one discharging pump and system is precipitated.
9. a kind of sodium chloride ammonium chloride according to claim 6 divides the device of salt crystallization processes, which is characterized in that the chlorine
It includes secondary heater, secondary cycle pump, second-stage separator, two level discharging pump, two level thickener, two to change ammonium crystal system is precipitated
Grade centrifuge, secondary mother liquor tank and two level discharging pump, the side wall of the second-stage separator be equipped with successively from top to bottom feed inlet one,
Feed inlet two and feed inlet three are equipped with secondary cycle pipe between the feed inlet two and the feed inlet of the secondary heater；
Waste liquid is pumped into the secondary cycle pipe by the level-one discharging pump, and wherein gas phase enters in the second-stage separator, liquid phase
Into in the secondary heater；Material in the secondary heater is delivered to the feed inlet by secondary cycle pump
One；Material in the second-stage separator is delivered to through the two level discharging pump in the two level thickener；
The feed end of the discharge end of the second-stage separator and the two level thickener is equipped with two level return duct, is convenient for the two level
Partial Liquid Phase is converted into gas phase when liquid phase in separator is delivered to the two level thickener through the two level discharging pump, and gas phase is just
Enter in second-stage separator from the two level return duct；
The two-stage centrifugal machine is used to the material in the two level thickener being separated by solid-liquid separation, and liquid enters the secondary mother liquor
Tank is pumped into the primary separator through the first charging aperture through the two level discharging pump and continues circulating and evaporating concentration.
10. a kind of sodium chloride ammonium chloride according to claim 9 divides the device of salt crystallization processes, which is characterized in that described
Two level thickener is equipped with the low-temperature receiver that can cool down.
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| CN110372007A (en) * | 2019-07-25 | 2019-10-25 | 山东亿盛实业股份有限公司 | The device and method of continuous separating ammonium chloride and sodium chloride |
| CN111003866A (en) * | 2019-12-06 | 2020-04-14 | 安徽晨晰洁净科技有限公司 | Waste salt concentration treatment device |
| CN112142068A (en) * | 2020-09-07 | 2020-12-29 | 湖北兴福电子材料有限公司 | Method for producing high-purity ammonium chloride from industrial-grade ammonium chloride |
| CN114132950A (en) * | 2021-11-30 | 2022-03-04 | 衡阳爱洁科技股份有限公司 | Method for preparing ammonium chloride by co-production of sodium bicarbonate |
| CN114477230A (en) * | 2022-02-17 | 2022-05-13 | 常州大学 | Method for separating alkali salt through chemical sublimation-temperature-changing crystallization in Hou's combined alkali preparation |
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| CN114477230A (en) * | 2022-02-17 | 2022-05-13 | 常州大学 | Method for separating alkali salt through chemical sublimation-temperature-changing crystallization in Hou's combined alkali preparation |
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